CN106039932A - Process and system for removing carbon dioxide in natural gas - Google Patents
Process and system for removing carbon dioxide in natural gas Download PDFInfo
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- CN106039932A CN106039932A CN201610378002.3A CN201610378002A CN106039932A CN 106039932 A CN106039932 A CN 106039932A CN 201610378002 A CN201610378002 A CN 201610378002A CN 106039932 A CN106039932 A CN 106039932A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20484—Alkanolamines with one hydroxyl group
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20489—Alkanolamines with two or more hydroxyl groups
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a process for removing carbon dioxide in natural gas. The process includes the following steps that firstly, after natural gas feed gas is subjected to preliminary removal through a first amine liquid absorption tower, coarsely filtered natural gas is obtained; then the coarsely filtered natural gas obtained in above step is subjected to fine removal through a second amine liquid absorption tower, and the natural gas is obtained. According to the characteristic of the natural gas feed gas that components change dynamically, a two-level amine liquid absorption and purification series connection process is adopted, the problem of removal of a high content of carbon dioxide in the feed gas components is effectively solved, the application range and capacity of processes and equipment in a factory are remarkably improved, applicability of a whole purification is wider, the processing capacity is higher, more guarantee is provided for processing precision, and by the adoption of the series connection process, it can be guaranteed that the content of carbon dioxide in the purified feed gas is 50 ppm or below.
Description
Technical field
The present invention relates to natural gas production technical field, be specifically related to the removing process of a kind of carbon dioxide in natural with
Removing system, particularly relates to the removing process of high-load carbon dioxide and removing system in a kind of natural gas.
Background technology
The definition of common " natural gas ", is to define from the narrow sense of energy point of view, refers to natural containing in stratum
Hydro carbons and the mixture of non-hydrocarbon gases, be high-grade fuel and industrial chemicals, mainly make fuel, white carbon black, chemistry can be manufactured
Medicine and liquefied petroleum gas, the propane of production, butane are also the important source material of modern industry.Natural gas is mainly by gaseous state low molecule
Hydrocarbon and non-hydrocarbon gas mixing composition, main component alkane, wherein methane accounts for the overwhelming majority, separately has a small amount of ethane, propane and fourth
Alkane, the most typically has hydrogen sulfide, carbon dioxide, nitrogen and aqueous vapor and a small amount of carbon monoxide and the rare gas of trace.Natural gas is made
For high-quality, the fuel of cleaning and important industrial chemicals, its range of application is increasingly wider, and industrial development paces are constantly accelerated.Closely
Nian Lai, China's natural gas exploration has major progress, in succession develops some important gas reservoirs, but this also result in natural gas and produces
Problems, wherein CO in natural gas _ raw material gas2Content height, be one of them major issue.
CO2Existence bring much harm to the conveying of natural gas and deep processing.First, CO2Too high levels can reduce sky
The calorific value of right gas and throughput of pipeline.If do not removed, unit is amassed heat produced by combustion of natural gas and can be substantially reduced.Its
Secondary, CO2Too high levels, during low temperature, it can become solid separation, thus blocks pipeline.It addition, natural gas is being carried out deep cooling
Adding man-hour, the temperature of natural gas is extremely low, can block again deep freeze refrigeration plant, causes deep cold worked instability.3rd, CO2Corrosion is also
It is the serious problems that can not be ignored.CO in the presence of aqueous solution, in natural gas2Equipment, pipeline can be caused
Serious corrosion.Therefore must be to CO2Remove.
CO in conventional removing natural gas2Method mainly have solvent absorption (include alcohol amine absorption process, hot potash method,
Physical solvent process), membrane separation process, several big classes such as membranes, cryogenic fractionation and pressure swing adsorption method, the wherein acid impurities master in natural gas
If H2S and CO2, and alcohol amine absorption process is at removing CO2While can be by H2S removes.
In the real-world operation of chemical plant, the natural gas of gaseous state purifies technological process through desulfurization, decarburization, dehydration etc..Purify
After gas in sulfur content :≤1ppm；Carbon dioxide content :≤50ppm；Water content≤1ppm；Desulfurization, dewatering process are the most ripe
Apply in chemical plant, in decarbonizing process carbon dioxide content by less than 3% being removed to≤technique of 50ppm is the most basicly stable.
But when in natural gas containing great amount of carbon dioxide, during such as content more than 3%, to remove and reach≤the content of 50ppm, technique
System is just difficult to, even if can realize, its stability and persistence also are difficult to ensure.But natural after cleaning system
In gas, carbon dioxide content is higher than≤50ppm, is also easy to cause follow-up cryogenic system to block, and whole system cannot be run, often
Start stop system, increases equipment operating cost, has a strong impact on factory's benefit.
Therefore, how to provide the removing process of carbon dioxide in a kind of natural gas _ raw material gas, a kind of stable, hold
The removing process of high-load carbon dioxide in the natural gas that continuous property is strong, it has also become the most numerous natural gas manufacturers are urgently to be resolved hurrily
One of problem.
Summary of the invention
In view of this, the technical problem to be solved in the present invention is to provide the de-of carbon dioxide in a kind of natural gas _ raw material gas
Except technique and system, the removing process of high-load carbon dioxide and system in a kind of natural gas, it is de-that the present invention provides
Except the technique of carbon dioxide in natural gas _ raw material gas, it is possible to sufficiently ensure that whole system stable and continuous is properly functioning, it is to avoid be
Unite frequent start stop system, reduce equipment operating cost, it is ensured that factory economy benefit.
The invention provides the removing process of a kind of carbon dioxide in natural, comprise the following steps:
A) by natural gas _ raw material gas after de-at the beginning of the first amine absorption tower, coarse filtration natural gas is obtained；
B) coarse filtration natural gas above-mentioned steps obtained, after the second amine absorption tower loss of essence, obtains natural gas；
Carbon dioxide content >=3% in described natural gas _ raw material gas.
Preferably, in described amine absorption tower, amine liquid consists of the one in MEA, DEA, TEA, DIPA, DGA and MDEA
Or it is multiple.
Preferably, the amine liquid in described first amine absorption tower consists of MEA, DEA, TEA, DIPA, DGA and MDEA；
The concentration of the amine liquid in described first amine absorption tower is 48%～52%.
Preferably, the amine liquid in described second amine absorption tower consists of MEA, DEA, TEA, DIPA, DGA and MDEA；
The concentration of the amine liquid in described second amine absorption tower is 40%～45%.
Preferably, described first amine absorption tower includes that first touches film net；
The described first mesh number touching film net is 100～300 mesh.
Preferably, described second amine absorption tower includes that second touches film net；
The described second mesh number touching film net is 400～600 mesh.
Preferably, the amine liquid in described first amine absorption tower, after the first amine liquid Analytic Tower regeneration, returns the first amine
Liquid absorption tower is reused；
Amine liquid in described second amine absorption tower, after the second amine liquid Analytic Tower regeneration, returns the second amine absorption tower
Reuse.
Preferably, the carbon dioxide content in described natural gas _ raw material gas is 5%～37%；
The gas treatment amount of described natural gas _ raw material gas is (15～100) * 104Nm3/d。
The invention provides the removing system of a kind of carbon dioxide in natural, including the first amine absorption tower, the second amine
Liquid absorption tower, natural gas _ raw material gas air inlet pipeline, natural gas _ raw material gas air inlet control metering device, coarse filtration natural gas escape pipe
Road and natural gas outlet pipe；
It is provided with natural gas _ raw material gas air inlet on described natural gas _ raw material gas air inlet pipeline and controls metering device；
The air inlet of described natural gas _ raw material gas air inlet pipeline and the first amine absorption tower bottom is connected；
The gas outlet of described first amine absorption column overhead is connected with one end of described coarse filtration natural gas outlet pipe；
The other end of described coarse filtration natural gas outlet pipe is connected with the air inlet of described second amine absorption tower bottom
Connect；
The gas outlet of described second amine absorption column overhead is connected with described natural gas outlet pipe.
Preferably, the first amine liquid Analytic Tower, the second amine liquid Analytic Tower are also included；
The described waste liquid import of the first amine lyolysis analysis top of tower exports phase with the amine liquid of described first amine absorption tower bottom
Connect, the regenerated amine liquid outlet of described first amine lyolysis analysis tower bottom and the amine liquid import phase of described first amine absorption top of tower
Connect；
The described waste liquid import of the second amine lyolysis analysis top of tower exports phase with the amine liquid of described second amine absorption tower bottom
Connect, the regenerated amine liquid outlet of described second amine lyolysis analysis tower bottom and the amine liquid import phase of described second amine absorption top of tower
Connect.
The invention provides the removing process of a kind of carbon dioxide in natural, comprise the following steps, first by natural gas
Unstripped gas, after de-at the beginning of the first amine absorption tower, obtains coarse filtration natural gas；Coarse filtration above-mentioned steps obtained again is natural
Gas, after the second amine absorption tower loss of essence, obtains natural gas；Carbon dioxide content >=3% in described natural gas _ raw material gas.
Compared with prior art, the present invention is after Discussion on Technology, simulation calculating, substantial amounts of test and creative selection, for natural
This underground mineral resources of gas unstripped gas has the advantages that component dynamically changes, and uses two-stage amine absorption to purify tandem process,
Effectively solve the removing problem of high-load carbon dioxide in feed gas composition, significantly improve technique in factory, equipment
Subject range and the ability of adaptation, make the whole cleaning system suitability more extensive, disposal ability is higher, and processing accuracy more has guarantor
Barrier；And the content of carbon dioxide is at below 50ppm, energy in unstripped gas to use the tandem process of the present invention can ensure after purification
Enough sufficiently ensure that the stable and continuous of whole system, especially aftertreatment systems is properly functioning, improve whole production system
Stability and persistence, it is to avoid the frequent start and stop of system, reduce equipment operating cost, it is ensured that factory economy benefit, more
It is suitable for industrialized great production.Test result indicate that, the removing process of the carbon dioxide in natural that the present invention provides and removing system
System, is 100*10 in natural gas _ raw material gas treating capacity4Nm3In the case of/d, still ensure that dioxy in the unstripped gas after process
Change carbon content less than or equal to 50ppm.
Accompanying drawing explanation
The general flow chart of the removing system of the carbon dioxide in natural that Fig. 1 provides for the present invention.
Detailed description of the invention
In order to be further appreciated by the present invention, below in conjunction with embodiment, the preferred embodiment of the invention is described, but
Should be appreciated that these describe simply as to further illustrate the features and advantages of the present invention rather than to the claims in the present invention
Limit.
The all raw materials of the present invention and equipment, be not particularly limited its source, that commercially buy or according to this area
Prepared by the conventional method known to technical staff.
The all raw materials of the present invention, are not particularly limited its purity, present invention preferably employs the purity that this area is conventional.
The invention provides the removing process of a kind of carbon dioxide in natural, comprise the following steps:
A) by natural gas _ raw material gas after de-at the beginning of the first amine absorption tower, coarse filtration natural gas is obtained；
B) coarse filtration natural gas above-mentioned steps obtained again, after the second amine absorption tower loss of essence, obtains natural gas；
Carbon dioxide content >=3% in described natural gas _ raw material gas.
The definition of described natural gas _ raw material gas is not particularly limited by the present invention, with raw material well known to those skilled in the art
The natural gas that natural gas or dampness, the i.e. natural gas well are produced, without the unstrpped gas before refining, also referred to as
" dampness ".Removing process of the present invention can be the most applicable for the natural gas _ raw material gas of conventional carbon dioxide content
Carbon dioxide content in the natural gas _ raw material gas of high carbon dioxide content, described natural gas _ raw material gas can be to be more than or equal to
3% or more than or equal to 5%, it is also possible to be 5%～50%, it is also possible to be 10%～45%, or be 15%～37%.This
Bright form the amine liquid in described amine absorption tower is not particularly limited, and those skilled in the art can be according to actual production feelings
Condition, unstripped gas quality and product quality select and adjust, and the present invention is to improve the most de-removal efficiency, and described amine liquid is inhaled
Receiving in tower, amine liquid composition is preferably MEA (monoethanolamine), DEA (diethanolamine), TEA (triethanolamine), DIPA (diisopropanol
Amine), one or more in DGA (diglycolamine) and MDEA (N methyldiethanol amine), more preferably MEA, DEA, TEA,
DIPA, DGA and MDEA.
The present invention first by natural gas _ raw material gas after de-at the beginning of the first amine absorption tower, obtain coarse filtration natural gas.
Described first amine absorption tower is not particularly limited by the present invention, with well known to those skilled in the art for natural
The amine absorption tower of gas unstripped gas desulfurization and decarburization, those skilled in the art can be according to practical condition, raw material makings
Amount and product quality select and adjust.The concentration of amine liquid in described first amine absorption tower is limited by the present invention the most especially
System, those skilled in the art can select according to practical condition, unstripped gas quality and product quality and adjust, this
Invention is preferably mass concentration, and the present invention is to improve the first de-effect of the first amine absorption tower, in described first amine absorption tower
The concentration of amine liquid be preferably 48%～52%, more preferably 48.5%～51.5%, more preferably 49%～52%, most preferably
It is 50%～51%.
The circulation technology of amine liquid in described first amine absorption tower is not particularly limited by the present invention, those skilled in the art
Can select according to practical condition, unstripped gas quality and product quality and adjust, the present invention is for improving the first amine
The utilization rate of amine liquid in liquid absorption tower, it is achieved continuous and stable production, the amine liquid in described first amine absorption tower is through the first amine
After the regeneration of liquid Analytic Tower, return the first amine absorption tower and reuse, i.e. amine liquid is carrying out depriving hydrogen sulphide to natural gas _ raw material gas
While carbon dioxide removal, return to absorption tower after being re-fed in Analytic Tower regeneration, thus realize the continuous of integrated artistic
Operating.
The present invention is to touching film net in described first amine absorption tower, the i.e. first mesh number touching film net is not particularly limited, this
Skilled person can select according to practical condition, unstripped gas quality and product quality and adjust, the present invention
For improving the first de-effect of the first amine absorption tower, the described first mesh number touching film net is preferably 100～300 mesh, more preferably
130～270 mesh, more preferably 150～250 mesh, most preferably 200 mesh.
The air inflow of described natural gas _ raw material gas is not particularly limited by the present invention, and those skilled in the art can be according to reality
The border condition of production, unstripped gas quality and product quality select and adjust, the removing process that the present invention provides, i.e. two-stage amine
Liquid absorption cleaning tandem process, the treating capacity of the natural gas _ raw material gas that can reach can be (15～100) * 104Nm3/ d, it is possible to
Think (20～100) * 104Nm3/ d, it is also possible to for (30～90) * 104Nm3/ d, or (40～70) * 104Nm3/d。
The requirement of described coarse filtration carbon dioxide in natural content is not particularly limited by the present invention, people in the art
Member can select according to practical condition, unstripped gas quality and product quality and adjust, and the present invention is for ensureing entirety
Being normally carried out and final carbon dioxide in natural content conformance with standard, coarse filtration natural gas of the present invention of removing process
In carbon dioxide content be preferably less than equal to 4% or less than or equal to 3%, it is also possible to for 50ppm～3%, it is also possible to for
500ppm～2.5%, or be 0.5%～2%.
The coarse filtration natural gas that above-mentioned steps is obtained by the present invention again, after the second amine absorption tower loss of essence, obtains natural
Gas, i.e. natural gas _ raw material gas after desulfurization and decarburization.
Described second amine absorption tower is not particularly limited by the present invention, with well known to those skilled in the art for natural
The amine absorption tower of gas unstripped gas desulfurization and decarburization, those skilled in the art can be according to practical condition, raw material makings
Amount and product quality select and adjust.The concentration of amine liquid in described second amine absorption tower is limited by the present invention the most especially
System, those skilled in the art can select according to practical condition, unstripped gas quality and product quality and adjust, this
Invention is preferably mass concentration, and the present invention is to improve the first de-effect of the second amine absorption tower, in described second amine absorption tower
The concentration of amine liquid be preferably 40%～45%, more preferably 41%～44%, more preferably 41.5%～43.5%, most preferably
It is 42%～43%.
The circulation technology of amine liquid in described second amine absorption tower is not particularly limited by the present invention, those skilled in the art
Can select according to practical condition, unstripped gas quality and product quality and adjust, the present invention is for improving the second amine
The utilization rate of amine liquid in liquid absorption tower, it is achieved continuous and stable production, the amine liquid in described second amine absorption tower is through the second amine
After the regeneration of liquid Analytic Tower, return the second amine absorption tower and reuse, i.e. amine liquid is carrying out depriving hydrogen sulphide to natural gas _ raw material gas
While carbon dioxide removal, return to absorption tower after being re-fed in Analytic Tower regeneration, thus realize the continuous of integrated artistic
Operating.
The present invention is to touching film net in described second amine absorption tower, the i.e. second mesh number touching film net is not particularly limited, this
Skilled person can select according to practical condition, unstripped gas quality and product quality and adjust, the present invention
For improving the first de-effect of the second amine absorption tower, the described second mesh number touching film net is preferably 400～600 mesh, more preferably
430～570 mesh, more preferably 450～550 mesh, most preferably 500 mesh.
The air inflow of described coarse filtration natural gas is not particularly limited by the present invention, and those skilled in the art can be according to reality
The border condition of production, unstripped gas quality and product quality select and adjust, the removing process that the present invention provides, i.e. two-stage amine
Liquid absorption cleaning tandem process, the treating capacity of the coarse filtration natural gas that can reach can be (5～65) * 104Nm3/ d, it is also possible to
For (10～65) * 104Nm3/ d, it is also possible to for (20～55) * 104Nm3/ d, or (30～45) * 104Nm3/d。
The requirement of described carbon dioxide in natural content is not particularly limited by the present invention, ripe with those skilled in the art
Standard carbon dioxide content after the natural gas decarburization known, the present invention be ensure overall removing process be normally carried out and
Final carbon dioxide in natural content conformance with standard, the carbon dioxide content in coarse filtration natural gas of the present invention is preferably
Less than or equal to 50ppm, it is also possible to for less than or equal to 49ppm, or it is less than or equal to 48ppm.
Above-mentioned steps of the present invention provides the removing process of a kind of carbon dioxide in natural, the present invention is directed to natural gas former
Expecting that in gas, dynamically change is big, the problem that especially carbon dioxide content is high, through Discussion on Technology, simulation calculating, substantial amounts of examination
Test and after creative selection, the present invention proposes the removing process of high-load carbon dioxide in a kind of natural gas, use two-stage clean
Change Cascade System technique in order to solve the removing problem of high-load carbon dioxide in component.First class purification system is by two in gas
Content of carbon oxide is removed to less than 3% by about 50%, the most slightly takes off cleaning system；Secondary purification system is again by the two of content 3%
Carbonoxide is removed to, less than or equal to 50ppm, be called for short loss of essence purification process.The taking off for high-load carbon dioxide that the present invention provides
Except technique, making the whole cleaning system suitability more extensive, disposal ability is higher, and processing accuracy is more secure.It is specially adapted to
Process gas flow more than 20*104Nm3The chemical plant scale that the carbon dioxide in natural high-load of/d (200,000 sides/sky) processes,
Can sufficiently ensure that whole system stable and continuous is properly functioning, it is to avoid the frequent start stop system of system, reduce equipment operating cost,
Ensure factory economy benefit.
Present invention also offers the removing system of a kind of carbon dioxide in natural, including the first amine absorption tower, second
Amine absorption tower, natural gas _ raw material gas air inlet pipeline, natural gas _ raw material gas air inlet control metering device, coarse filtration natural gas are given vent to anger
Pipeline and natural gas outlet pipe；
It is provided with natural gas _ raw material gas air inlet on described natural gas _ raw material gas air inlet pipeline and controls metering device；
The air inlet of described natural gas _ raw material gas air inlet pipeline and the first amine absorption tower bottom is connected；
The gas outlet of described first amine absorption column overhead is connected with one end of described coarse filtration natural gas outlet pipe；
The other end of described coarse filtration natural gas outlet pipe is connected with the air inlet of described second amine absorption tower bottom
Connect；
The gas outlet of described second amine absorption column overhead is connected with described natural gas outlet pipe.
Concrete specification, arrangement and the material etc. of described natural gas _ raw material gas air inlet pipeline are limited by the present invention the most especially
System, those skilled in the art can select according to practical condition, unstripped gas quality and product quality and adjust, this
Invention is for ensureing to realize to produce continuously and system controls, and described natural gas _ raw material gas air inlet pipeline is that to be preferably provided with natural gas former
Material gas air inlet controls metering device.The present invention controls the concrete specification of metering device, installation to described natural gas _ raw material gas air inlet
Require and model etc. be not particularly limited, those skilled in the art can according to practical condition, unstripped gas quality and
Product quality selects and adjusts.
The air inlet of natural gas _ raw material gas air inlet pipeline of the present invention and the first amine absorption tower bottom is connected, this
Bright above-mentioned concrete link position being not particularly limited, those skilled in the art can be according to practical condition, unstripped gas
Quality and product quality select and adjust, and realize the desulfurization and decarburization of natural gas _ raw material gas as optimal case with maximization.
The gas outlet of the first amine absorption column overhead of the present invention and one end of described coarse filtration natural gas outlet pipe
Being connected, above-mentioned concrete link position is not particularly limited by the present invention, and those skilled in the art can be according to actual production
Situation, unstripped gas quality and product quality select and adjust, to maximize the desulfurization and decarburization realizing natural gas _ raw material gas
For optimal case.
The other end of coarse filtration natural gas outlet pipe of the present invention and the air inlet of described second amine absorption tower bottom
Mouth is connected, and above-mentioned concrete link position is not particularly limited by the present invention, and those skilled in the art can be raw according to reality
Product situation, unstripped gas quality and product quality select and adjust, de-to maximize the desulfurization realizing natural gas _ raw material gas
Carbon is optimal case.
The gas outlet of the second amine absorption column overhead of the present invention is connected with described natural gas outlet pipe, the present invention
Above-mentioned concrete link position is not particularly limited, and those skilled in the art can be according to practical condition, raw material makings
Amount and product quality select and adjust, and realize the desulfurization and decarburization of natural gas _ raw material gas as optimal case with maximization.
Other specifications and the setting of described first amine absorption tower are not particularly limited, with people in the art by the present invention
The specification of the amine absorption tower known to Yuan or arrange, those skilled in the art can be according to practical condition, unstripped gas
Quality and product quality select and adjust, and the present invention is to ensure being carried out continuously of decarbonization, desulfuration, improves carbon dioxide
Removal efficiency, the diameter of described first amine absorption tower is preferably 800～1200m, more preferably 850～1150m, more preferably
900～1100m, most preferably 1000m；Described first amine absorption Ta Neitanei touches film device external diameter, and i.e. first touches outside film device
Footpath, preferably 700～1100mm, more preferably 750～1050mm, more preferably 800～1000mm, most preferably 900mm.
Other specifications and the setting of described second amine absorption tower are not particularly limited, with people in the art by the present invention
The specification of the amine absorption tower known to Yuan or arrange, those skilled in the art can be according to practical condition, unstripped gas
Quality and product quality select and adjust, and the present invention is to ensure the quality of natural gas after decarbonization, desulfuration, improves titanium dioxide
The removal efficiency of carbon, the diameter of described second amine absorption tower is preferably 300～700m, more preferably 350～650m, more preferably
It is 400～600m, most preferably 500m；Described second amine absorption Ta Neitanei touches film device external diameter, and i.e. second touches outside film device
Footpath, preferably 200～600mm, more preferably 250～550mm, more preferably 300～500mm, most preferably 400mm.
The present invention is to improve the utilization rate of amine liquid in the second amine absorption tower, it is achieved continuous and stable production, described removing system
System the most also includes the first amine liquid Analytic Tower, the second amine liquid Analytic Tower.
Of the present invention first amine lyolysis analysis top of tower waste liquid import preferably with described first amine absorption tower bottom
Amine liquid outlet be connected, described first amine lyolysis analysis tower bottom regenerated amine liquid outlet preferably with described first amine absorption tower top
The amine liquid import in portion is connected；Above-mentioned concrete link position is not particularly limited by the present invention, and those skilled in the art are permissible
Select according to practical condition, unstripped gas quality and product quality and adjust, realizing gas material to maximize
Desulfurization and decarburization and the amine liquid of gas are recycling as optimal case.
Of the present invention second amine lyolysis analysis top of tower waste liquid import preferably with described second amine absorption tower bottom
Amine liquid outlet be connected, described second amine lyolysis analysis tower bottom regenerated amine liquid outlet preferably with described second amine absorption tower top
The amine liquid import in portion is connected；Above-mentioned concrete link position is not particularly limited by the present invention, and those skilled in the art are permissible
Select according to practical condition, unstripped gas quality and product quality and adjust, realizing gas material to maximize
Desulfurization and decarburization and the amine liquid of gas are recycling as optimal case.
The present invention removes other devices of system to carbon dioxide in described natural gas _ raw material gas or follow up device does not has
Limit especially, those skilled in the art can carry out selecting according to practical condition, unstripped gas quality and product quality and
Adjusting, realize natural gas purification as preferred version maximizing, natural gas outlet pipe of the present invention is follow-up with cooling
Device is connected, and the most again after dehydration device dehydration, enters follow-up processing flow.
See the general flow chart of the removing system of the carbon dioxide in natural that Fig. 1, Fig. 1 provide for the present invention.
Above-mentioned steps of the present invention provides removing process and the removing system of a kind of carbon dioxide in natural, and particularly one
Kind for the removing process of high-load carbon dioxide in natural gas and system.The present invention calculates, in a large number through Discussion on Technology, simulation
Experiment and creative select after, have the advantages that component dynamically changes for this underground mineral resources of natural gas _ raw material gas,
Use two-stage amine absorption to purify tandem process and system, effectively solve the de-of high-load carbon dioxide in feed gas composition
Except problem, significantly improve technique in factory, the subject range of equipment and adaptation ability, make the whole cleaning system suitability more
Adding extensively, disposal ability is higher, and processing accuracy is more secure；And use the tandem process of the present invention and system can ensure only
After change in unstripped gas the content of carbon dioxide at below 50ppm, it is possible to sufficiently ensure whole system, especially subsequent treatment system
The stable and continuous of system is properly functioning, improves stability and the persistence of whole production system, it is to avoid the frequent start and stop of system,
Reduction equipment operating cost, it is ensured that factory economy benefit, is more suitable for industrialized great production.Test result indicate that, the present invention carries
The removing process of the carbon dioxide in natural of confession and removing system, be 100*10 in natural gas _ raw material gas treating capacity4Nm3/ d's
In the case of, still ensure that in the unstripped gas after process, carbon dioxide content is less than or equal to 50ppm.
In order to be further appreciated by the present invention, below in conjunction with titanium dioxide in the natural gas _ raw material gas that the present invention is provided by embodiment
Removing process and the system of carbon are described in detail, and protection scope of the present invention is not limited by the following examples.
Embodiment 1
Day output 500,000 side
Natural gas _ raw material gas component sees table 1, and table 1 is the constituent content of the present embodiment natural gas _ raw material gas.
As shown in Table 1, in natural gas _ raw material gas, carbon dioxide content is 37.1687%, and hydrogen sulfide content is 0.4541%.
The natural gas pump of above-mentioned content is depressed into 6MPa, sends into a diameter of 1000m via natural gas _ raw material gas air inlet pipeline
The first amine absorption tower, air inflow is 50*104Nm3/d；Amine liquid in first amine absorption tower consists of MDEA and desalted water,
The concentration of amine liquid is 50%, and the tactile film mesh number in absorption tower is 200 mesh, and external diameter is 900mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the first amine absorption tower from bottom to top, obtain coarse filtration sky
So gas, is then entered loss of essence by the gas outlet of the first amine absorption column overhead via coarse filtration natural gas outlet pipe and purifies system
System；Wherein the amine liquid in the first amine absorption tower exports via the amine liquid bottom absorption tower and sends into the first amine liquid Analytic Tower, passes through
After the regeneration of amine liquid Analytic Tower, then the regenerated amine liquid outlet by the first amine lyolysis analysis tower bottom, return to the first amine absorption tower
Recycle.
The coarse filtration natural gas via that above-mentioned steps obtains is sent into the of a diameter of 500m by coarse filtration natural gas outlet pipe
Diamidogen liquid absorption tower, air inflow is 33*104Nm3/d；Amine liquid in second amine absorption tower consists of MDEA and desalted water, amine liquid
Concentration be 40%, the tactile film mesh number in absorption tower is 500 mesh, and external diameter is 400mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the second amine absorption tower from bottom to top, obtain natural gas,
I.e. natural gas _ raw material gas after desulfurization and decarburization, then by the gas outlet of the second amine absorption column overhead via natural gas outlet pipe
After sending into follow-up chiller and dehydration device process, then carry out follow-up flow process；The wherein amine liquid in the second amine absorption tower
Export via the amine liquid bottom absorption tower and send into the second amine liquid Analytic Tower, after amine liquid Analytic Tower regenerates, then by the second amine liquid
Regenerated amine liquid outlet bottom Analytic Tower, returns to the second amine absorption tower and recycles.
The natural gas obtaining above-mentioned steps of the present invention detects, the sulfur content of the second amine absorption column overhead gas outlet
For 1ppm, outlet carbonated amount is 7ppm, and the above-mentioned removing system stability that the present invention provides is good, and seriality is good,
Parameter is stable.
Embodiment 2
Day output 300,000 side
Natural gas _ raw material gas component sees table 2, and table 2 is the constituent content of the present embodiment natural gas _ raw material gas.
| Component | Percentage by volume % | Component | Percentage by volume % |
| Methane | 66.80 | Pentane | 0.05 |
| Ethane | 5.34 | Normal hexane | 0.01 |
| Propane | 2.27 | Normal heptane | 0.01 |
| Iso-butane | 0.44 | Carbon dioxide | 23.81 |
| Normal butane | 0.47 | Nitrogen | 0.73 |
| Isopentane | 0.07 | Hydrogen sulfide | 0 |
As shown in Table 2, in natural gas _ raw material gas, carbon dioxide content is 23.81%, and hydrogen sulfide content is 0.
The natural gas pump of above-mentioned content is depressed into 6MPa, sends into a diameter of 800m's via natural gas _ raw material gas air inlet pipeline
First amine absorption tower, air inflow is 30*104Nm3/d；Amine liquid in first amine absorption tower consists of MDEA and desalted water, amine
The concentration of liquid is 50%, and the tactile film mesh number in absorption tower is 200 mesh, and external diameter is 700mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the first amine absorption tower from bottom to top, obtain coarse filtration sky
So gas, is then entered loss of essence by the gas outlet of the first amine absorption column overhead via coarse filtration natural gas outlet pipe and purifies system
System；Wherein the amine liquid in the first amine absorption tower exports via the amine liquid bottom absorption tower and sends into the first amine liquid Analytic Tower, passes through
After the regeneration of amine liquid Analytic Tower, then the regenerated amine liquid outlet by the first amine lyolysis analysis tower bottom, return to the first amine absorption tower
Recycle.
The coarse filtration natural gas via that above-mentioned steps obtains is sent into the of a diameter of 450m by coarse filtration natural gas outlet pipe
Diamidogen liquid absorption tower, air inflow is 19.8*104Nm3/d；Amine liquid in second amine absorption tower consists of MDEA and desalted water, amine
The concentration of liquid is 42%, and the tactile film mesh number in absorption tower is 500 mesh, and external diameter is 350mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the second amine absorption tower from bottom to top, obtain natural gas,
I.e. natural gas _ raw material gas after desulfurization and decarburization, then by the gas outlet of the second amine absorption column overhead via natural gas outlet pipe
After sending into follow-up chiller and dehydration device process, then carry out follow-up flow process；The wherein amine liquid in the second amine absorption tower
Export via the amine liquid bottom absorption tower and send into the second amine liquid Analytic Tower, after amine liquid Analytic Tower regenerates, then by the second amine liquid
Regenerated amine liquid outlet bottom Analytic Tower, returns to the second amine absorption tower and recycles.
The natural gas obtaining above-mentioned steps of the present invention detects, the sulfur content of the second amine absorption column overhead gas outlet
For 1ppm, exporting carbonated amount 12ppm, and the above-mentioned removing system stability that the present invention provides is good, seriality is good, ginseng
Number is stable.
Embodiment 3
Day output 200,000 side
Natural gas _ raw material gas component sees table 3, and table 3 is the constituent content of the present embodiment natural gas _ raw material gas.
As shown in Table 3, in natural gas _ raw material gas, carbon dioxide content is 16.545%, and hydrogen sulfide content is 0.
The natural gas pump of above-mentioned content is depressed into 6MPa, sends into a diameter of 600m's via natural gas _ raw material gas air inlet pipeline
First amine absorption tower, air inflow is 20*104Nm3/d；Amine liquid in first amine absorption tower consists of MDEA and desalted water, amine
The concentration of liquid is 50%, and the tactile film mesh number in absorption tower is 200 mesh, and external diameter is 500mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the first amine absorption tower from bottom to top, obtain coarse filtration sky
So gas, is then entered loss of essence by the gas outlet of the first amine absorption column overhead via coarse filtration natural gas outlet pipe and purifies system
System；Wherein the amine liquid in the first amine absorption tower exports via the amine liquid bottom absorption tower and sends into the first amine liquid Analytic Tower, passes through
After the regeneration of amine liquid Analytic Tower, then the regenerated amine liquid outlet by the first amine lyolysis analysis tower bottom, return to the first amine absorption tower
Recycle.
The coarse filtration natural gas via that above-mentioned steps obtains is sent into the of a diameter of 400m by coarse filtration natural gas outlet pipe
Diamidogen liquid absorption tower, air inflow is 13.2*104Nm3/d；Amine liquid in second amine absorption tower consists of MDEA and desalted water, amine
The concentration of liquid is 45%, and the tactile film mesh number in absorption tower is 500 mesh, and external diameter is 300mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the second amine absorption tower from bottom to top, obtain natural gas,
I.e. natural gas _ raw material gas after desulfurization and decarburization, then by the gas outlet of the second amine absorption column overhead via natural gas outlet pipe
After sending into follow-up chiller and dehydration device process, then carry out follow-up flow process；The wherein amine liquid in the second amine absorption tower
Export via the amine liquid bottom absorption tower and send into the second amine liquid Analytic Tower, after amine liquid Analytic Tower regenerates, then by the second amine liquid
Regenerated amine liquid outlet bottom Analytic Tower, returns to the second amine absorption tower and recycles.
The natural gas obtaining above-mentioned steps of the present invention detects, the sulfur content of the second amine absorption column overhead gas outlet
For 1ppm, outlet carbonated amount is 20ppm, and the above-mentioned removing system stability that the present invention provides is good, and seriality is good,
Parameter is stable.
Comparative example 1
Day output drops to less than the 50% of conventional treatment amount, 100,000 sides
Natural gas _ raw material gas component sees table 4, and table 4 is the constituent content of the present embodiment natural gas _ raw material gas.
As shown in Table 4, in natural gas _ raw material gas, carbon dioxide content is 37.1687%, and hydrogen sulfide content is 0.4541%.
The natural gas pump of above-mentioned content is depressed into 6MPa, sends into a diameter of 1000m via natural gas _ raw material gas air inlet pipeline
The first amine absorption tower, air inflow is 10*104Nm3/d；Amine liquid in first amine absorption tower consists of MDEA and desalted water,
The concentration of amine liquid is 50%, and the tactile film mesh number in absorption tower is 200 mesh, and external diameter is 900mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the first amine absorption tower from bottom to top, obtain coarse filtration sky
So gas, is then sent into follow-up chiller with de-by the gas outlet of the first amine absorption column overhead via natural gas outlet pipe
After water device processes, then carry out follow-up flow process；Wherein the amine liquid in the first amine absorption tower goes out via the amine liquid bottom absorption tower
Mouth sends into the first amine liquid Analytic Tower, after amine liquid Analytic Tower regenerates, then is gone out by the regenerated amine liquid of the first amine lyolysis analysis tower bottom
Mouthful, return to the first amine absorption tower and recycle.
The natural gas obtaining above-mentioned steps of the present invention detects, the sulfur content of the second amine absorption column overhead gas outlet
For 6ppm, outlet carbonated amount is 6%, and above-mentioned removing system stability is poor, easily causes follow-up cryogenic system and blocks up
Filling in, whole system cannot be run, frequent start stop system, poor continuity, parameter fluctuation of service.
Comparative example 2
Day output 300,000 side
Natural gas _ raw material gas component sees table 5, and table 5 is the constituent content of the present embodiment natural gas _ raw material gas.
As shown in Table 5, in natural gas _ raw material gas, carbon dioxide content is 37.1687%, and hydrogen sulfide content is 0.4541%.
The natural gas pump of above-mentioned content is depressed into 6MPa, sends into a diameter of 1000m via natural gas _ raw material gas air inlet pipeline
The first amine absorption tower, air inflow is 30*104Nm3/d；Amine liquid in first amine absorption tower consists of MDEA and desalted water,
The concentration of amine liquid is 60%, and the tactile film mesh number in absorption tower is 200 mesh, and external diameter is 1200mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the first amine absorption tower from bottom to top, obtain coarse filtration sky
So gas, is then entered loss of essence by the gas outlet of the first amine absorption column overhead via coarse filtration natural gas outlet pipe and purifies system
System；Wherein the amine liquid in the first amine absorption tower exports via the amine liquid bottom absorption tower and sends into the first amine liquid Analytic Tower, passes through
After the regeneration of amine liquid Analytic Tower, then the regenerated amine liquid outlet by the first amine lyolysis analysis tower bottom, return to the first amine absorption tower
Recycle.
The coarse filtration natural gas via that above-mentioned steps obtains is sent into the of a diameter of 600m by coarse filtration natural gas outlet pipe
Diamidogen liquid absorption tower, air inflow is 19.8*104Nm3/d；Amine liquid in second amine absorption tower consists of MDEA and desalted water, amine
The concentration of liquid is 55%, and the tactile film mesh number in absorption tower is 300 mesh, and external diameter is 700mm.
After natural gas _ raw material gas carries out primary decarbonization, desulfuration in the second amine absorption tower from bottom to top, obtain natural gas,
I.e. natural gas _ raw material gas after desulfurization and decarburization, then by the gas outlet of the second amine absorption column overhead via natural gas outlet pipe
After sending into follow-up chiller and dehydration device process, then carry out follow-up flow process；The wherein amine liquid in the second amine absorption tower
Export via the amine liquid bottom absorption tower and send into the second amine liquid Analytic Tower, after amine liquid Analytic Tower regenerates, then by the second amine liquid
Regenerated amine liquid outlet bottom Analytic Tower, returns to the second amine absorption tower and recycles.
The natural gas obtaining above-mentioned steps of the present invention detects, the sulfur content of the second amine absorption column overhead gas outlet
For 3ppm, outlet carbonated amount is 4%, and above-mentioned removing system stability is poor, easily causes follow-up cryogenic system
Blocking, whole system cannot be run, and frequent start stop system, seriality is poor, parameter fluctuation of service.
The explanation of above example is only intended to help to understand method and the core concept thereof of the present invention.It is right to it should be pointed out that,
For those skilled in the art, under the premise without departing from the principles of the invention, it is also possible to the present invention is carried out
Some improvement and modification, these improve and modify in the protection domain also falling into the claims in the present invention.
Described above to the disclosed embodiments, makes professional and technical personnel in the field be capable of or uses the present invention.
Multiple amendment to these embodiments will be apparent from for those skilled in the art, as defined herein
General Principle can realize without departing from the spirit or scope of the present invention in other embodiments.Therefore, the present invention
It is not intended to be limited to the embodiments shown herein, and is to fit to and principles disclosed herein and features of novelty phase one
The widest scope caused.
Claims (10)
1. the removing process of a carbon dioxide in natural, it is characterised in that comprise the following steps:
A) by natural gas _ raw material gas after de-at the beginning of the first amine absorption tower, coarse filtration natural gas is obtained；
B) coarse filtration natural gas above-mentioned steps obtained, after the second amine absorption tower loss of essence, obtains natural gas；
Carbon dioxide content >=3% in described natural gas _ raw material gas.
Removing process the most according to claim 1, it is characterised in that in described amine absorption tower, amine liquid consist of MEA,
One or more in DEA, TEA, DIPA, DGA and MDEA.
Removing process the most according to claim 2, it is characterised in that the amine liquid in described first amine absorption tower consists of
MEA, DEA, TEA, DIPA, DGA and MDEA；
The concentration of the amine liquid in described first amine absorption tower is 48%～52%.
Removing process the most according to claim 2, it is characterised in that the amine liquid in described second amine absorption tower consists of
MEA, DEA, TEA, DIPA, DGA and MDEA；
The concentration of the amine liquid in described second amine absorption tower is 40%～45%.
Removing process the most according to claim 1, it is characterised in that described first amine absorption tower includes that first touches film
Net；
The described first mesh number touching film net is 100～300 mesh.
Removing process the most according to claim 1, it is characterised in that described second amine absorption tower includes that second touches film
Net；
The described second mesh number touching film net is 400～600 mesh.
Removing process the most according to claim 1, it is characterised in that the amine liquid in described first amine absorption tower is through
After one amine liquid Analytic Tower regeneration, return the first amine absorption tower and reuse；
Amine liquid in described second amine absorption tower, after the second amine liquid Analytic Tower regeneration, returns the second amine absorption tower weight multiple
Use.
Removing process the most according to claim 1, it is characterised in that the carbon dioxide content in described natural gas _ raw material gas
It is 5%～37%；
The gas treatment amount of described natural gas _ raw material gas is (15～100) * 104Nm3/d。
9. the removing system of a carbon dioxide in natural, it is characterised in that include that the first amine absorption tower, the second amine liquid are inhaled
Receive tower, natural gas _ raw material gas air inlet pipeline, natural gas _ raw material gas air inlet control metering device, coarse filtration natural gas outlet pipe with
And natural gas outlet pipe；
It is provided with natural gas _ raw material gas air inlet on described natural gas _ raw material gas air inlet pipeline and controls metering device；
The air inlet of described natural gas _ raw material gas air inlet pipeline and the first amine absorption tower bottom is connected；
The gas outlet of described first amine absorption column overhead is connected with one end of described coarse filtration natural gas outlet pipe；
The other end of described coarse filtration natural gas outlet pipe is connected with the air inlet of described second amine absorption tower bottom；
The gas outlet of described second amine absorption column overhead is connected with described natural gas outlet pipe.
Removing system the most according to claim 9, it is characterised in that also include the first amine liquid Analytic Tower, the second amine lyolysis
Analysis tower；
The waste liquid import of described first amine lyolysis analysis top of tower exports with the amine liquid of described first amine absorption tower bottom and is connected,
The regenerated amine liquid outlet of described first amine lyolysis analysis tower bottom is connected with the amine liquid import of described first amine absorption top of tower；
The waste liquid import of described second amine lyolysis analysis top of tower exports with the amine liquid of described second amine absorption tower bottom and is connected,
The regenerated amine liquid outlet of described second amine lyolysis analysis tower bottom is connected with the amine liquid import of described second amine absorption top of tower.
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| CN111562247A (en) * | 2019-02-13 | 2020-08-21 | 中国石油天然气股份有限公司 | Hydrogen sulfide and carbon dioxide on-line analysis device and method |
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